Method for enhanced energy production from transforming, reducing and eliminating organic material and medical waste

ABSTRACT

A waste transformation and destruction apparatus includes a natural gas ignition system, a silica material bed, a heat transfer device, and a system for collecting plasma produced energy. A reaction formed by heat from ignition, carbon from the waste material, supercritical water, —OH radicals, and muons released from the silica bed transform the waste into a fuel. This fuel is more efficiently consumed by the complete combustion process resulting in near total elimination of the waste, increased energy production, and virtually no emissions.

CROSS-REFERENCE TO RELATED APPLICATION

This application is a continuation-in-part of U.S. patent applicationSer. No. 13/253,804, filed Oct. 5, 2011, which is incorporated byreference.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The invention is in the field of transformation of fossil fuels,biomass, medical waste and organic waste into energy production and thefield of reduction and elimination of medical waste and organic waste.

2. Review of Technology

Conventional energy production from organic fuel materials relies oncombustion of organic materials into their combustion products. The mostfavorable combustion products do not include carbon-carbon bonds andcarbon-hydrogen bonds because such products indicate incompletecombustion, and thereby there is still combustion potential that was notutilized for energy production. When combustion is incomplete, thereusually is some environmental concern for the organic combustionproducts, which can be desirable to clean or degrade before beingreleased from the combustion system. The incomplete combustion ofcarbon-containing fuels such as gasoline, diesel fuel, fuel oil, coal,wood, biomass and even natural gas can result in the generation ofpollutants such as carbon particulates, hydrocarbons, soot, oilysubstances, carbon monoxide (CO), and other pollutants. Such pollutantscollect in the atmosphere and can cause all manner of health problemsand smog.

For example, in response to pollution caused by gasoline-poweredinternal combustion engines, catalytic converters have been developedand mandated to reduce the levels of incomplete combustion pollutantsemitted into the environment by gasoline powered vehicles. Catalyticconverters are typically positioned in-line with the exhaust andmuffling system of an internal combustion engine and are generally ableto catalytically convert only trace amounts of the un-burnt hydrocarbonsand CO into CO₂ and water. Although modern catalytic converters can beused to convert trace amounts of un-burnt hydrocarbons and CO intocarbon dioxide (CO₂) and water, they are generally only feasible for usewith relatively clean burning systems such as gasoline-powered vehicles.

Additionally, industrial burners, such as those that burn coal, fueloil, or natural gas can also suffer from incomplete combustion. Inresponse to pollution controls directed to industrial burners,sophisticated scrubbers and after burners have been developed inattempts to reduce environmental pollution. However, these and otherpollution reduction means can be quite expensive, both in retrofittingolder industrial burners as well as in the fabrication of new ones. Noneof these existing systems result is a substantial reduction ofpollutants.

Incomplete combustion can also be problematic in the degradation ofbiological waste such as medical waste and animal corpses.Traditionally, disposal and degradation of biological waste has beenperformed by incineration and combustion of the organic materials withinthe waste. The disposal of medical waste in a manner that will notrelease dangerous pathogenic or disease-causing agents into theenvironment has always been a relatively expensive and difficult task.This is because it is necessary to first kill all pathogenic orpotentially pathogenic agents, and then completely destroy the tissue toprevent further rotting and decay of the tissue. Otherwise, the tissuecan provide a haven where later-introduced foreign pathogenic agents canthrive. For instance, it is inadequate to simply sterilize once-livinghuman tissue and then dispose of it like ordinary refuse where it willbe exposed to bacteria or other natural biodegradation agents. In theprocess of natural degradation, human infection-causing agents can findtheir way to the discarded human tissue, where they can thrive and thenreinfect others.

Sterilization of medical waste typically requires manual microwaving orautoclaving followed by incineration to destroy the biological waste.This process has proved inadequate as a means to ensure totaldestruction of all pathogenic agents, including viruses. This is becauseof the inability to achieve complete combustion or destruction of allviruses or other pathogenic agents before they find their way out thesmoke stack, or flue, of the incinerator. While incomplete combustionand degradation of biological waste may have different environmentalconsequences compared to incomplete combustion of organic fuels, it isstill desirable to obtain the complete degradation of the biologicalwaste for safety and avoidance of environmental concerns.

Accordingly, it would be advantageous to provide methods and systemsthat could effectively and inexpensively eliminate, or at leastsubstantially reduce, the quantity of un-burnt or partially burntcombustion products from organic fuels and biological waste in aneconomically feasible manner. It would also be advantageous to providemethods and systems for eliminating, or at least greatly reducing, thequantity of incomplete combustion products which would eliminate theneed for expensive catalysts, such as palladium, platinum and other rareand expensive metals. Additionally, it would be advantageous to providemethods and systems that can degrade biological waste and completelydestroy infectious and potentially harmful biological materials.

BRIEF SUMMARY OF THE INVENTION

The present invention relates to methods and systems for transformationof organic waste, medical waste, coal, fossil fuels, and biomass intothermal energy and the substantial reduction and near elimination ofthese materials. The invention eliminates the conventional need formanual use of microwave energy followed by autoclave incineration todestroy medical waste, which can require over two hours at a temperatureof over 2000° F. and produces a stream of unburned waste, pollutants,soot and odors.

The disclosed process eliminates essentially 100% of all organic waste,medical waste, toxic waste, polymeric materials such as PVC (polyvinylchloride) plastics, and efficiently transforms them into a newintermediate fuel, which helps to complete the combustion process andmore completely reduce and eliminate the materials with no significantemissions. Combustion typically involves intermediate transformations ofsolid or liquid organic materials into gases, which react with oxygen toform heat and gaseous combustion products. The disclosed processinitially transforms organic materials into a new intermediate type ofhigh powered gaseous fuel that is completely consumed and converted intoenergy, eliminating emissions. It does this by more efficiently crackingcellulosic molecular bonds and other inorganic elements found in organicmatter and separating the intermediate gaseous compounds withinmilliseconds of the beginning of the reaction. CO (carbon monoxide),sulfur, and all 17 inorganic elements typically present in emissions arecracked, completely combusted, and eliminated. This produces completecombustion and the elimination of all pollutants.

The transformation of organic matter to a new super fuel and CompleteCombustion™ was first discovered by Tom Maganas in 2002. The researchwas testing a process for elimination of soot and other organicemissions from a diesel engine utilizing hydroxyl (—OH) radicals,supercritical water, and muon radicals at high top compression andtemperature. Research was then extended to test the process foreliminating medical waste and organic waste.

The experimental chamber for medical waste disposal is a cylindricalreactor 16 inches in diameter and 44 inches tall that contains a bed ofpebbles, silica that releases OH radicals into the plasma and a cradlecage that suspends the waste above the plasma reaction. A monomolecularnano film coats the entire interior. This nano film is deposited duringinitial use of the reactor and thereafter helps to catalyze thereactions. Ignition is provided by natural gas, which raises thetemperature of the reaction chamber from room temperature to an initialignition temperature of about 540° C.

After the reactor is heated to 540° C., the cage containing medicalwaste is lowered into the reaction chamber through a hole in the top andsuspended above the silica. The gas fire is stopped. Heat in the reactorbegins to transform the medical waste, which releases gases. Gaseswithin the chamber interact with the silica to form hydroxyl radicals,supercritical water, muons, and other highly reactive free radicalspecies within the reaction chamber. The nano film enhances the reactiveenvironment.

After initially dropping, the temperature again rises within a fewminutes and stabilizes at 540° C. The intermediate gases produced fromthe transformed organic waste create a new intermediate fuel thatcombusts completely and quickly increases the temperatures in thereactor, which can reach up to 940° C. At this point, heat generation isself-sustaining without further input of flammable gas. Depending on themedical waste load, temperatures above 540° C. can be maintained forabout 60 minutes. When the temperature drops, that is an indication thatthe fuel has been consumed. The process consumes 100% of organic waste,typically leaving about 20% incombustible valuable inorganic matter as abyproduct with zero emissions.

Eight months of research involving organic medical waste led to adecision to test coal energy against organic waste energy using the sametest methods as in medical waste tests. Soft and hard Appalachian coalwere divided, separated and tested with ten pound coal loads using thesame methodology. The coal produced sufficient heat energy to maintain asteady, self-sustaining temperature of 500° C. to 570° C. for 90 minutesbefore running out, with essentially zero odors and atmosphericemissions. Depending on the ash content of the coal, the tests caused aweight loss of about 80% weight loss, leaving about 20% of incombustibleinorganic matter as a byproduct.

Anthracite coal has a BTU (British thermal units) content of about11,000 BTU per pound, while lignite coal contains about has 6,000 BTUper lb. By comparison, cow leg bones used as “medical waste” have a BTUcontent of less than 100 BTU per lb, yet the experiments demonstrated arepeatable temperature rise to 990° C. when using cow leg bones, whilethe maximum coal temperature was 570° C. The disclosed process was ableto more efficiently and controllably extract thermal energy from bothcoal and cow leg bones compared to conventional combustion methods. Theforegoing claims are fully documented, and surpass Clean Air Actrequirements.

The inventive methods and systems convert fossil fuel, biomass and/ormedical waste into thermal energy and efficiently destroy medical wasteby means of a plasma within the reaction chamber, which destroys organicmatter, including medical and other toxic wastes, such as polyvinylchloride (PVC), with a weight loss of 80% to 90% within 60 minuteswithout burning or producing soot, odors, fumes, and toxic gas emissionsto the atmosphere as are commonly produced using conventionalincineration.

A heat generation reactor can be configured for efficient and cleanconversion of organic materials into heat energy. Such a reactor caninclude: a reaction chamber; a thermally insulating monomolecular nanofilm permanently installed on an interior surface of the reactionchamber; an initial heat generation source located within the reactionchamber; an air source fluidly coupled with the reaction chamber; andsilica particles located within the reaction chamber. The monomolecularfilm is comprised of dwarfed aligned molecules of carbon havingdimensions of 30 angstroms by 50 angstroms, which elongate to 70angstroms at high pressure. Though highly thermally insulating, themonomolecular film may behave as a semiconductor to produce electricalenergy (e.g., as a plasma).

Thus, the present invention relates to the manufacture of asemiconductor material for use in making microprocessors, computerchips, transistors, or photovoltaic solar cells. The semiconductormaterial comprises a substrate, such as those commonly used in thesemiconductor industry, and a single layer of a monomolecular nano filmcomprised of aligned carbon molecules having dimensions of 30 angstromsby 50 angstroms and that elongate to 70 angstroms at high pressureresulting in substantial increase in temperature resistance, andoperating capabilities

The silica particles, when exposed to heat from the heat generationsource and organic fuel generate and with air flowing up from thebottom, generate a reactive atmosphere of hydroxyl radicals,supercritical water, muons and/or other reactive species. A supportelement is configured to support an organic fuel material above thesilica and includes at least one support surface with one or moreapertures that permit passage of air to increase plasma efficiency andassist in the complete combustion of the fuel.

A method for efficiently and cleanly converting organic material intoheat energy can include: providing a reactor as described herein;introducing a biological or other organic material into the reactionchamber so as to be located above the silica; introducing heat andairflow into the reaction chamber so as to generate hydroxyl radicals,supercritical water, muons and/or other reactive species that caninteract with the organic material; and converting the organic materialinto heat energy.

Clean energy can be produced using a heat exchanger element thermallycoupled with the reaction chamber and providing components forconverting heat energy into electrical energy. For example, electricitycan be generated from a steam generator thermally coupled with the heatexchanger element.

These and other embodiments and features of the present invention willbecome more fully apparent from the following description and appendedclaims, or may be learned by the practice of the invention as set forthhereinafter.

BRIEF DESCRIPTION OF THE DRAWINGS

To further clarify the above and other advantages and features of thepresent invention, a more particular description of the invention willbe rendered by reference to specific embodiments thereof which areillustrated in the appended drawings. It is appreciated that thesedrawings depict only illustrated embodiments of the invention and aretherefore not to be considered limiting of its scope. The invention willbe described and explained with additional specificity and detailthrough the use of the accompanying drawings in which:

FIG. 1 is a perspective view of an embodiment of a reactor in whichorganic material can be efficiently converted into heat energy.

FIG. 2 is a cross-sectional view of an embodiment of a reactor equippedwith heat exchangers.

FIG. 3 is a cross-sectional view of an embodiment of a reactor forefficiently converting organic material into heat energy.

FIGS. 4A-4D include various view of different embodiments of supportelements that can hold and retain organic material above a catalyticmedia during conversion of the organic material to heat energy within areactor.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

I. Introduction

Generally, the present invention relates to improved methods and systemsfor conversion of organic materials, such as organic fuels andbiological waste, into thermal energy which, in turn, can be used tomake electrical energy. The methods and systems can be used forincreasing energy production from organic fuel materials as well as forincreasing the ability to disinfect and completely destroy organic wastematerials, particularly biological and medical wastes such as corpses.The present invention utilizes the ability of a catalytic media, such assilica or alumina, to generate highly reactive hydroxyl radicals,supercritical water, muons and other reactive species in the presence ofan organic fuel heated to efficiently transform the fuel into heatenergy. Such conversion may be carried out in a single reaction chamberor multiple reaction chambers, at a relatively constant temperaturerange, and in a one-step process. This allows for the efficientconversion of organic materials into heat energy without the attendantproblems of high temperature formation of NO_(x) and SO_(x) typicallyproduced during high temperature combustion of organic materials.

The terms “activate” and “activated” are meant to refer a condition inwhich the catalytic media (e.g., silica and/or alumina particles) areable to produce a “reactive atmosphere” of hydroxyl radicals and otherreactive species capable of degrading and extracting heat energy fromorganic material, such as a carbon-containing fuel or biological waste.

The terms “biological waste,” “medical waste,” “animal tissue,” or“human tissue” are meant to refer any biological, microbe, animal orhuman tissue or cells, or biological components thereof. Such materialstypically comprise protein, fat, blood, and bone mass. Because blood ismost water, biological waste is difficult to burn using conventionalcombustion methods.

The term “reactive atmosphere” is meant to refer to the condition withinthe reaction chamber, and possibly surrounding areas and conduits, thatinclude a localized concentration of highly reactive hydroxyl radicals,supercritical water, muons and/or other reactive molecular fragments,free radicals or species capable of degrading or otherwise reacting withorganic materials to efficiently convert them into heat energy.

The terms “carbon-containing fuel,” “organic fuel material,” or“biological materials” are meant to refer to any organic material thatgenerate and/or release energy when combusted or burned, usually in theform of heat, light or a combination thereof. The term “fossil fuel” isa subset of “carbon-containing fuel” and includes coal, oil, naturalgas, derivatives of coal, natural gas and oil, and the like. Non-fossilorganic fuels include alcohols, fuels derived from alcohols or otherfermentation products, wood, biomass and the like.

The term “reaction chamber” shall be broadly construed to include anyapparatus capable of holding therein a catalytic media, such as silicaand/or alumina, and that provides appropriate conditions that result information of the reactive atmosphere for degrading and convertingorganic materials into heat energy.

The terms “degrade” or “degradation” refer to processes by which organicmaterials or incomplete combustion products such as soot, hydrocarbons,CO, tissues, cells, biological fluids, and oily substances are at leastpartially broken down or eliminated to yield lesser organic substances.It includes complete combustion of gases into carbon dioxide, water andother clean reaction products. It also includes any reaction in whichCO, CO₂, carbon or hydrocarbons are converted into other, less pollutingforms of carbon or other substances. Degradation of some biologicalmaterials, such as biological tissue, can generate a small amount ofash, which can be collected for sentimental reasons or appropriatelydiscarded.

The term “suspended” is meant to indicate that at least a portion of thecatalytic particles are slightly elevated and/or separated by risinggases such that they are not at rest in a state of natural particlepacking density. Suspending the particles leaves them in a lesscompacted state. This suspended or separated elevated state yieldsparticles with surfaces that are more accessible and available forcontact with the diffused heated gases rising through the particleswithin the reaction chamber. Increased surface contact with diffusedheated gases is believed to increase the ability of the catalyticparticles to generate the reactive degrading atmosphere. Failure topartially separate the particles results in less efficient and uniformconversion of organic material into heat energy.

The term “operating temperature” is meant to refer to the temperature atwhich hydroxyl radicals, supercritical water, muons and/or other freeradicals or reactive substances, molecular fragments or reactive speciescapable of degrading and converting organic materials into heat energyare generated by a catalytic media such as silica and/or alumina.

The term “portable” is meant to refer to the ability of the devices andsystems used to carry out the methods of the present invention, asembodied in certain embodiments, to be capable of being moved throughouta building or medical or research facility or industrial site or energyplant or wherever needed. This movement of the device or system might beby simply carrying, wheeling by means of a supporting stand equippedwith rollers or wheels, or moving by means of moving equipment (e.g., aforklift or small crane), the important feature being that a portabledevice or system is not primarily a fixture as the term is commonlyunderstood.

II. Device and System

A. Example Operating Parameters

The inventive system was tested using cow leg bones, pork hearts, andneck bones with meat, as well as toxic PVC plastic pipes (e.g., 4 feetof 2 inch PVC pipe) which normally produce deadly fumes when heated orburned. Coal of various forms was also converted into thermal energyusing the disclosed apparatus and methods. The inventive reactor reducedthe PVC to three ounces of white and black particles with zero odorswithin 30 minutes. Another test was performed using 30 lbs. of 3×2 inchcow leg bones with a weight loose of 80%. One previously reacted bonedropped accidentally from a work table and crumbled. These tests havebeen repeated with similar results each time.

The emission tests recorded a CO₂ (carbon dioxide) reading of initially4%. Emissions were gradually reduced to zero by the end of the test run.The initial HC (hydrocarbon) and CO (carbon monoxide) emissions of 40ppm were reduced to 4 ppm (parts per million). By comparison, combustionof diesel oil normally yields 4000 ppm of CO and 15% CO₂. The 80-90%reduction in weight with extremely low emissions provides evidence thatthe biomass was efficiently used as fuel.

According to one embodiment, the inventive process uses natural gas toreach an initial temperature of 540° C. and air injected into thereactor to start reactions involving the biomass and/or organic wasteand the reactive media particles in the reaction chamber. Natural gasflow is cut off when a temperature of 540° C. is reached but heatproduction continues with the biomass or reactive organic wasteproducing increased temperature without producing a flame. Thecontinuing reactions transform the waste into thermal energy and reducebone weight by 80% to 90% and the PVC plastic weight is reduced by over95%. 50 pages of paper were also combusted and their weight was reducedby over 85%. The paper showed no signs of actually burning and producedno emissions and the print remained visible but when touched the paperbroke like snowflakes.

The initial Maganas Plasma Process™ was pioneered by Thomas C. Maganasand Allen Harrington, and a nano molecule that formed a monomolecularfilm discovered in Chemical Vapor Deposition (CVD) led to the discoveryof a diesel catalytic converter. The monomolecular nano film includeselongated dwarf shaped carbon molecules with a precise size, and shapewhich was 30 Å (angstroms) by 50 Å. Increased pressure increased itssize to 70 Å with resistance to cracking, while other nanomoleculescrack merely by a touch. Maganas and Harrington filled a U.S. patent in1991 and won a patent in 1992 for the film. Johannes GutenbergUniversity in Mainz, Germany claimed discovery and identified theidentical Maganas monomolecular nano film with their advanced electronmicroscope that matched our nanomaterial as to size, shape, and itsresistance to 400,000 atmospheres of pressure before cracking. Theirphotos fully matched our nanomaterial that formed the monomolecularfilm, which is an important aspect in reduction of diesel emissions andorganic waste and reduce emissions by 99.995%. Maganas has been awarded12 patents by the United States Patent Office and has other patentspending. We have additional foreign patents, and have invested severalmillions of dollars into the Research and Development of these newtechnologies prompted by the Maganas and Harrington discovery of —OHradicals and the nano formation of monomolecular film.

A fully developed and functional prototype system is now operating atthe Maganas Laboratories. Located in Carson, Calif., this firstgeneration system was developed to serve as the functional proof ofconcept of the technology exhibiting the following highlights:

-   -   1. Conversion of low energy grade cow bones, soft body tissue,        plastics, and many other forms of organic matter into sustained        temperatures of 420° C.-600° C. without flames with about 5% of        the fuel that normally would be required;    -   2. Demonstrated ability to convert paper and PVC plastic into        sustained temperatures of 500° C.-700° C. in the absence of        combustion and with a 90% reduction of mass weight and 99.995%        emission reduction with zero odors throughout the test during        transformation, and the particles that is left over on        completion.

The Maganas Plasma Process™ is based upon inducing plasma to form and toallow hydroxyl radical reactions in a reactor coated with amonomolecular film with an open top that allows atmosphere penetrationwithout affecting the process.

Tom Maganas process of eliminating diesel engine emissions with ahydrocarbon diesel catalytic converter that eliminates 99.995% of allemissions from diesel engines with a ⅔ reduction in fuel consumption andan increase of power. The two key elements of the Maganas catalyticconverter is hydroxyl radicals, and the monomolecular nano film, whichtogether produce reactions to crack 17 inorganic elements found indiesel fuel that equaled 1,451 ppm (parts per million), and also reducedsulfur to a sulfate ash element that could not be weighed by theanalyzing scientist. This also permanently deposited the monomolecularnano film onto the interior surface of the reactor. Diesel fuel beinginjected into compression with —OH radicals and monomolecular nano filmreactions that crack 1,451 ppm of the inorganic elements from diesel toform a fuel to increase power and decrease fuel consumption by ⅔ occurby breaking the carbon chains and releasing supercritical water as a gasby separating inorganic elements. One would have to conclude that thestandard ⅔ drop in fuel emissions means they are consumed as fuel andmatch Maganas Plasma transformation organic of medical waste.

B. Example Structures and Methods

In the following detailed description, reference is made to theaccompanying drawings, which form a part hereof. In the drawings,similar symbols typically identify similar components, unless contextdictates otherwise. The illustrative embodiments described in thedetailed description, drawings, and claims are not meant to be limiting.The features of the embodiments and figures described and shown hereincan be used and combined with other features of other embodiments aswell as figures. Other embodiments may be utilized, and other changesmay be made, without departing from the spirit or scope of the subjectmatter presented herein. It will be readily understood that the aspectsof the present disclosure, as generally described herein, andillustrated in the Figures, can be arranged, substituted, combined,separated, and designed in a wide variety of different configurations,all of which are explicitly contemplated herein.

In one embodiment, FIG. 1 illustrates an embodiment of a reactor 100that can be used for destruction and efficient conversion of organicsubstances 123 into heat energy. For example, the reactor 100 can beused for enhancing the combustion or conversion of organic fuelmaterials into heat energy as well as destroying biological waste,tissues, or corpses and other organic substances. In yet anotherexample, the reactor 100 can be used for efficient energy production bycatalytic degradation and conversion of various organic substances, suchas organic fuels and biological waste.

The reactor 100 can include a reaction chamber 112 containing a heatgeneration source 122 (e.g., a gas flame or electrical heating element),an air flow source 120, a base support 118, an airflow diffuser 116, acatalytic media 114, and a support element 102 configured for supportingan organic material 123 at a distance (D) above the catalytic media 114.The support element 102 includes a support surface with one or moreapertures 103 so that gases can pass therethrough and deliver reactivespecies produced by the catalytic media to the organic material 123. Thereaction chamber 112 can include a void space 104 between the supportelement 102 and a top filter 130 and/or an exhaust conduit 128. Thedepth of catalytic media 114 need only be sufficient to produce areactive atmosphere of reactive hydroxyl radicals or other reactivespecies and can be as little as 1 inch and as high as 1 foot, with about2-7 inches being preferred, and about 2-5 inches being most preferred.

The positioning of the support element 102 above the catalytic media 114at a distance D allows for the reaction chamber 112 to be capable offacilitating substantially complete degradation and conversion oforganic materials (e.g., organic fuels and biological waste) into heatenergy. Additionally, the support element 112 keeps the organic material123 from falling into the catalytic media 114. The reaction chamber 112is generally enclosed or sealed except for where air is introduced intothe bottom of the reaction chamber 112 to suspend or separate the media114. Additionally, the reaction chamber 112 can include an inlet 124 sothat the organic material 123, alone or contained by the support element102, can be introduced into the reaction chamber 112. Also, the reactionchamber 112 includes the exhaust conduit 128 so that resulting gasesand/or heat can be removed.

The catalytic media 114 can include sand-like particles of a materialsuch as silica sand, silica gel, hydroxylbastnasite, alumina, other —OHradical generating materials known in the art or which may be developed,and the like. Silica sand, silica gel, alumina, and mixtures thereof arepreferred media because of their low cost and exceptional performance inthe reaction chamber 112. The catalytic particles can have an averagesize (e.g., diameter or cross-sectional dimension) ranging from about0.1 mm to about 1 cm, more preferably from about 0.2 mm to about 5 mm,and most preferably from about 0.5 mm to about 2.5 mm.

The catalytic media 114 can consist essentially of silica, alumina, ormixtures thereof. The term “consist essentially of” should be understoodto mean that the catalytic media 114 can be particles that mainlyconsist of silica, alumina or mixtures thereof, but they may includeminor quantities of impurities such as metals and ash typically found insilica and/or alumina. It is believed that the silica and/or alumina,when properly activated in the presence of sufficient heat and moisture,produce a localized reactive atmosphere of highly reactive hydroxylradicals, muons and/or other reactive species or molecular fragments,which are able to degrade and convert organic materials into heatenergy.

Moreover, whereas the silica and/or alumina are believed to beresponsible for the formation of a reactive atmosphere that includesabundant hydroxyl radicals such that expensive catalysts such aspalladium and platinum are not necessary, inclusion of such materials inminor amounts would be within the scope of the present invention so longas the silica and/or alumina are activated and able to produce thereactive atmosphere.

It may be advantageous to select catalytic particles that have arelatively high specific surface area. The high specific surface areacan be achieved by particle size distribution as well as porosity of theparticles. It is believed that it is at the surface of the catalyticparticles where the reactive hydroxyl radicals or other reactive speciesor molecular fragments are generated. Accordingly, increasing thesurface area of the catalytic particles without increasing their weightallows for the use of a lower mass of particles while maintaining adesired level of reactivity with the organic material. Reduced weight isparticularly desirable in the present embodiment, since the reactionchamber 112 can be configured to be portable. The amount of particlesneeded may be significantly reduced when the grain size is reducedand/or the surface of the particles is made to be more irregular, bothof which tend to increase the specific surface area of the catalyticparticles.

The catalytic media 114 is shown to be positioned above an air diffuser116 which sits upon a base support 118. Optionally, the air diffuser 116and base support 118 can be combined into a single element that functionto both 1) support the catalytic media at a desired location within thereaction chamber 112 and 2) diffuse air passed through the reactionchamber 112 so that the airflow is sufficiently diffuse to substantiallyuniformly suspend or separate the catalytic media 114.

In one example, the air diffuser 116 can be a bed of pebbles, rock orparticles that are substantially larger than the catalytic media 114.The airflow rates for suspending the catalytic media will generallydepend on the size of the reaction chamber and/or the quantity oforganic material being converted. According to one embodiment, theairflow rate can range from about 1 ft³/min to about 500 ft³/min, morepreferably from about 5 ft³/min to about 250 ft³/min, and mostpreferably from about 10 ft³/min to about 100 ft³/min.

The air diffuser 116 can be configured to efficiently transfer heat withrespect to the airflow throughout the catalytic media 114 and reactionchamber 112. When the air diffuser 116 includes rocks, they can sit atopa support plate that functions as the base support 118. On the otherhand, the air diffuser 116 can be a support plate that has a sufficientamount and distribution of apertures that diffuse the air passedtherethrough. The air source 120 can be oriented with respect to the airdiffuser 116 and/or base support so that air introduced through the airdiffuser 116 can travel upward through the catalytic media 114 and notdownward and away from the catalytic media 114. The base support 118(e.g., support plate) can include a heat conductive material (e.g.,metal) for effective heat transfer when heat is used to regulate thetemperature of the reaction chamber 112.

An air source 120 blows forced air through the catalytic media 114 to apartially suspend and/or churn the catalytic media 114. An example of anair source 120 can include air jets from an air compressor. The air jetscan be located below or within the air diffuser 116 to facilitate a moredisperse airflow through the catalytic media 114. However, the air jetscan be situated directly within the catalytic media 114, typically inembodiments where an air diffuser 116 is not employed. Also, the airjets can be located below a base support 118 that has apertures that candiffuse the airflow.

The air that is introduced into the reaction chamber 112 by the airsource 120 can be heated to a desirable temperature. For example, theairflow from air jets may be preheated to approximately the desiredtemperature of the reaction chamber 112, or it may become heated bymeans of heat that radiates through the base support 118 and/or airdiffuser 116. Also, a heat generation source 122 can be provided in anorientation that provides a flame or electrical heating element as ameans for heating the base support 118 and/or air diffuser 116. The heatgeneration source 122 may include one or more burners that burn a carbonfuel source. Also, the heat generation source 122 can be an electricresistive heater or any other device that can transfer heat to the basesupport 118, air diffuser 116, catalytic media 114, or airflow from theair source 120.

In the instance where heated air is introduced into the reaction chamber112 (e.g., by air jets), the air may be preheated by a number of means,including electric heating means or radiant heating means heated by afuel such as natural gas, fuel oil, or coal, where it is desired to passpure air through the reaction chamber 112. However, it may be moreeconomical to simply introduce and burn natural gas within the reactionchamber 112 (e.g., within the catalytic media 114). Because natural gasproduces mainly water and carbon dioxide, it should not inhibit thereaction process within the reaction chamber 112. Generation of watervapor from natural gas may enhance the reactivity of the catalytic media114 through production of hydroxyl radicals. Other combustion gasesbesides natural gas can be used. Because the combustion gases arepreferably blended with introduced airflow in order to provide theproper temperature conditions, the air that is introduced into thereaction chamber 112 can include adequate oxygen in most cases. However,it is possible to enrich the air with pure oxygen if desired to increasethe reactivity within the reaction chamber 112.

The airflow through the catalytic media 114 should have sufficientvelocity and pressure to cause the catalytic media 114 to becomepartially suspended. In order to obtain the best and most efficientconversion of organic materials, it may be preferable to blow justenough air to cause adequate suspension of the media so that the supportelement 102 holding an organic material 123 remains a distance (D) overthe catalytic media 114 when suspended. Alternatively, the supportelement 102 can be adjusted a distance (D) from the top of the catalyticmedia 114 within the void space 104 in order to effect optimalconversion of the organic material 123. However, it should be consideredthat the less air that actually passes through the reaction chamber 112,while maintaining adequate suspension, will use less energy and producea lower quantity of resulting gases that are vented from the reactionchamber 112.

The reactor 100 can be equipped with means for introducing biologicalmaterials 123 into the reaction chamber 112, where the biologicalmaterials 123 can be packaged or loose on the support element 102. Thebiological materials 123 can be introduced into the reaction chamber 112while on the support element 102, or they can be placed onto a supportelement 102 already installed in the reaction chamber 112. Such a meanscan include an entrance 124 such as doors, ports, continuous inlets, orany other configuration that allows the biological materials 102, suchas solids or liquids, to be passed into the reaction chamber 112 toreside on the support element 102 during conversion. The entrance 124can be configured to be capable of quickly opening to receive thebiological material 123, and then closing in order to retain the heatwithin the reaction chamber 112. In an alternative embodiment, theentrance 124 may include a set of double doors to better retain heatwithin the reaction chamber 112, with a first door opening to allow theintroduction of the organic material within a pre-chamber (not shown),after which a second door opens up into the main reaction chamber 112.

In some instances, such as where very large pieces of biologicalmaterial (e.g., corpses) are introduced into the reaction chamber 112,it might be preferable to open the reaction chamber 112 through a lid126 covering the top of the reaction chamber 112. The lid 126 can beremoved from the main body 125 of the reaction chamber 112. In thatcase, it may be necessary to restore the temperature within the reactionchamber 112 by temporarily increasing the temperature of the air that isintroduced into the reaction chamber and/or increasing the heat producedby heat generation source 122.

The reactor 100 can include an exhaust conduit 128 positioned above thereaction chamber 112 so that produced gases can be released. Optionally,the exhaust conduit 128 can be located near the entrance 124 and/or thelid 126 at the top of the reaction chamber 112, which carries the gasesto an appropriate location for emission into the outside air. Heatwithin the waste gases can also be recycled back into the reactionchamber 112 by any appropriate method known to those of ordinary skillin the art, such as by heat exchange, to heat up the air introduced intothe reaction chamber 112, or by simply recirculating the gases back intothe reaction chamber 112 to ensure complete and efficient breakdown ofessentially all organic materials 123 and gases. This may be one meansof ensuring the complete conversion and/or destruction of any biologicalmaterials, such as viruses or pathogenic agents. Organic materials 123,such as carbon fuels, medical waste, viruses, bacteria, and the like,all are converted to a new fuel resulting in complete combusting anddestruction of all organic matter, viruses, and bacteria.

In one embodiment, a method for efficiently converting organic materialsinto heat energy can be performed with the reactor 100. The conversionmethod can be performed in a manner for enhancing energy production fromcarbon fuels, as well as for destroying both biological waste and animalor human corpses. According to one embodiment, the temperature withinreaction chamber 112 can be maintained in a range from about 350° C. toabout 600° C., more preferably at about 550° C. This temperature can beobtained at in the void space 104, such as at the support element 102 ata distance (D) above the catalytic media 114. This temperature can beinitially achieved by the heat generation source 120 and/or air source122. The heat generation source 120 can be extinguished and/or reducedin heat production once the organic material 123 begins to convert andproduce heat energy, and the air source 122 flow rate can be adjusted sothat the conversion of the organic material 123 to heat energy ismaintained. The conversion of the organic material 123 can be maintainedeven when the heat generation source 120 is deactivated. In part, it isthought that the conversion of the organic material 123 can bemaintained from the reactive species generated by the catalytic material114. Below a given conversion temperature, the conversion reaction maybe inhibited. Above a given conversion temperature, excess heat may beunnecessary and, therefore, inefficient.

The inventor has found that organic materials 123, such as carbon fuels,medical wastes, corpses, and other organic wastes, are efficientlyconverted by means of reactive species produced by the catalytic media114, which include reactive hydroxyl radicals, hydrogen oxides, muons,or other highly oxidative species. Because of the oxidative nature ofthe process for converting organic materials into heat energy, it may bepreferable to ensure that there is abundant oxygen within the air beingintroduced into the reaction chamber 112.

In one embodiment, biological materials may be encapsulated within anyappropriate encapsulation material capable of being converted in thesame manner as the biological material within the reaction chamber 112.For example, biological fluids and/or tissues can be retained within acombustible package. The combustible encapsulation material can includepaper, thin plastic bags, and the like.

In some cases it might be desirable to adjust the composition of theatmosphere within the reaction chamber 112. For example, it may bedesirable to increase the amount of oxygen within the reaction chamber112 by intermittently injecting oxygen in order to facilitate oxidationof a particular biological material. Most biological waste naturallycontain water, which can yield additional hydroxyl radicals during theprocess. Supplemental gas may be introduced together with the air bymeans of the air source 120 or other gaseous inlet.

FIG. 2 illustrates another embodiment of a reactor 200 that can be usedfor converting organic substances 223 into heat energy. The reactor 200can include a reaction chamber 212 containing a heat generation source222, an air source 220 with an air inlet 221, a base support 218configured to diffuse airflow, a catalytic media 214, and an supportelement 202 configured to hold an organic material 223 at a distance (D)above the catalytic media 214 when suspended. The support element 202includes one or more apertures 203 so that gases can pass therethroughand deliver reactive species to convert the organic material 223.

Suspension of catalytic media 214 within the reaction chamber 212maintains a void space 204 between the catalytic media 214 particles andthe support element 202. The support element 202 is configured to retainthe organic material 223 above the catalytic media 214 through thevarious stages of conversion.

The reaction chamber 212 can include an inlet 224 so that the organicmaterial 223, alone or contained by the support element 202, can beintroduced into the reaction chamber 212. The reaction chamber 212 canbe configured with a lid 226 that can be entirely removed for loadinglarge organic materials 223 as well as the support element 202 into thereaction chamber 212.

Also, the reaction chamber 212 includes an exhaust conduit 228 so thatgases produced by conversion of the organic materials 223 can beremoved. The exhaust conduit 228 can include a capturing element 230that prevents escape of supercritical water from the reaction chamber.The reaction zone 216 can be located at or above the support element 202up to the capturing element 230.

The embodiment of the reactor bed device of FIG. 2 can be beneficialbecause the air can be blown into the reaction chamber 212 below theheat generation source 222 so that the air blown into the reactionchamber 212 by the air source 220 through the air inlet 221 blows pastthe heat source 222 so as to heat the airflow. The flame source 222 canalso heat the base support 218, which can in turn heat the airflow.

In one embodiment, the reaction chamber 212 can be operatively coupledwith an energy generator (not shown) such that the conversion of theorganic material 223 provides heat for energy production. The energygenerator may include a heat exchanger 290 that can be partially locatedwithin the reaction chamber 212. More particularly, the heat exchanger290 can be located within the reaction zone 216 so that heat fromconversion of organic material can heat a heat exchanger fluid 291. Theheated heat exchanger fluid 291 can then be used to convert heat energyto electrical energy as is well known, such as through steam generators.The number, orientation, location, or other parameter of the heatexchanger 290 can be modulated so that any number can be used and sothat the location of the heat exchanger 290 is optimum for heatexchange.

FIG. 3 illustrates another embodiment of a reactor 300 that can be usedfor conversion of organic materials 323 into heat energy. The reactor300 can include a reaction chamber 312 containing a heat generationsource 322 positioned below a base support 318 holding an airflowdiffuser 316, such that the heat generation source 322 can heat the basesupport 318 and airflow diffuser 316. An air source 320 with an airinlet 321 can be located within the airflow diffuser 316 so that the airblown into the reaction chamber 312 can be heated and diffused. Acatalytic media 314 is located on or above the airflow diffuser 316 sothat the diffused airflow can suspend the catalytic media 314. Ansupport element 302 configured for holding an organic material 323 ispositioned within the reaction chamber 312 at a distance (D) over thecatalytic media 314 when suspended. The support element 302 includes oneor more apertures (not shown) that permit reactive gases to passtherethrough and deliver reactive species to convert the organicmaterial 323. The support element 302 is configured to include a heatexchanger component 390 so that a heat exchanger fluid 391 can passthrough the support element 302. Sufficient heat is generated fromreacting and converting organic material 323 so that the heat exchangercomponent 390 is sufficiently heated from the organic material 323.

The reactor 300 can also include an inlet 324 so that the organicmaterial 323 can be introduced into the reaction chamber 312 and placedon the support element 302. Also, the reaction chamber 312 can beconfigured with a lid 326 that can be entirely removed for loading largequantities of organic materials 323 as well as the support element 302into the reaction chamber 312.

Also, the reaction chamber 312 includes an exhaust conduit 328 so thatexhaust gases containing reaction products and/or heat can be removed.The exhaust conduit 328 can include a filter 330 so that particulates,such as reaction product particulates, do not pass through the exhaustconduit 328, but may be retained within the reaction chamber 312 so thatsuch particulates fully combust within a reaction zone 316 and heat theheat exchanger component 390. The reaction zone 316 can be located at oraround the support element 302.

FIGS. 4A-4D illustrate various embodiments of an support element 402that can hold an organic material for conversion within a reactionchamber. As shown in FIG. 4A, the support element 402 can be configuredas a substrate that includes one or more apertures 403 that extend froma top surface 405 to a bottom surface so as to allow for reactive gasesto pass therethrough and convert the organic material located on the topsurface 405.

FIG. 4B includes a support element 402 that is similar to one shown inFIG. 1A, except that the support element 402 includes one or more heatexchanger conduits 492. The apertures 403 (shown up close in FIG. 4C toinclude fluid permeable member 411) are distributed around the heatexchanger conduits 492 so as to not intersect therewith. As such, theapertures 403 and heat exchanger conduits 492 are mutually exclusive ofeach other and not fluidly coupled.

FIG. 4D shows a support element 402 that has two or more elevatedsupport substrates 402 a and 402 b. Each elevated support substrate 402a and 402 b can be configured as any support element 402 describedherein. As shown, one or more support members 413 are used to couple thetwo or more elevated support substrates 402 a,b together so that the topelevated support substrate 402 a is located above the bottom elevatedsupport substrate 402 b while being retained within a reaction zone.Alternatively, the two or more elevated support substrates 402 a,b canbe independently coupled with an inside wall of a reaction chamber sothat support members 413 are not required. When multiple elevatedsupport substrates 402 a,b are included and mounted within a reactionchamber, one or more doors or access ports can be included between theelevated support substrates for access to the support substrates 402a,b, especially lower support substrates 402 b.

In one embodiment, the support element can be a distance of from about 1inch to about 24 inches above the catalytic media when suspended, orfrom about 2 inches to about 12 inches, or from about 3 inches to about8 inches, or from about 4 inches to about 5 inches. Also, thesedistances can be the distance from the organic material on a top surfaceof the support element from the suspended catalytic media. Additionally,these distances can be from a bottom elevated support in amulti-elevated support embodiment. Particular examples of the distancethe elevated support and/or organic material can be from 2-3 inches,more preferably from 4-5 inches, even more preferably from about 5-8inches, and most preferably from 9-12 inches. Previously, it was thoughtthat an organic material would have to be in physical contact with andsubmerged within the volume of catalytic particles in order to effectconversion or reaction of the organic materials from reactive speciesgenerated by the catalytic media. However, it has now been unexpectedlyand unpredictably found that an elevated support element can be used toretain the organic material above or outside the catalytic media so thatthe particles of the catalytic media do not actually contact the organicmaterial or its reaction products. Thus, now it is unexpectedly foundthat reactive species can be generated from the catalytic media, whichthen travel up to facilitate conversion of the organic material above oroutside the volume of catalytic media.

While the reactors described herein can be scaled up or down dependingon industrial or bench-top settings, the reaction chamber can beexemplified by a cross-sectional dimension of from about 1 foot to 10feet, or from about 1.5 feet to about 8 feet, or from about 2 feet toabout 6 feet, or from about 2.5 feet to about 5 feet, or from about 3feet to about 4 feet. The corresponding void space or reaction chamberheight for one of these cross-sectional dimensions can range from about3 feet to about 15 feet, or from about 3.25 feet to about 10 feet, orfrom about 3.5 feet to about 8 feet, or from about 4 feet to about 6feet, or about 5 feet. The reaction zone within the reaction chamber canbe at or above the support element or the surface containing an organicmaterial. When multiple elevated supports are included, there may bemultiple reaction zones. The height of the reaction zone can be lessthan about 24 inches above the elevated support, or less than about 12inches, or less than about 8 inches, or less than about 5 inches.Particular examples of the height of the reaction zone can be about 2-3inches around the organic material, more preferably from 4-5 inches,even more preferably from about 5-8 inches, and most preferably from9-12 inches around the organic material. It will be appreciated thatthese dimensions are exemplary for a bend scale model and would certainincrease when scaling up the unit (e.g. so as to have 2 to 500 times thecapacity of the bend scale version).

In a one embodiment, the catalytic media particles are suspended in afairly static condition against the force of gravity by means of airflowing upwards through the particles so that the support element withinthe reaction chamber retains the organic material at a distance (D)above the catalytic particles. Such airflow can be provided by any gaspressurizing means known in the art, including turbines, fans, pumps, orthe like. Suspending the catalytic particles greatly increases theactive surface area of the silica and/or alumina particles by separatingthem slightly and allowing for more gas-to-particle contact forproducing the reactive species that travel up to interact and convertthe organic material.

The conversion of the organic material provides heat to the reactionchamber within the reaction zone such that the temperature can bemaintained or even increased once gas supply to a flame source isreduced or stopped. The conversion of organic material can heat thecatalytic media, void space of the reaction chamber, and the reactionzone. The temperature obtained from conversion of the organic materialcan increase up to about 900° C., or up to about 750° C., or up to about600° C., or be maintained between about 400° C. to about 550° C. Highertemperatures are likely to be capable of being achieved. Thesetemperatures can be obtained with biological materials, coal, charcoalor other fuels as the organic material. However, other carbon fuelsources may be capable of producing even more heat and highertemperatures.

Because the catalytic media is a source for reactive species that aregenerated from the interaction of the catalytic particles, oxygen, andthe organic material, the catalytic media might be expected to breakdown over time, or become depleted as organic materials are convertedinto thermal energy. In fact, it appears that a measurable fraction ofthe catalytic media is broken down over time, although the amount isextremely small in comparison to the molar equivalents of organicmaterial being converted or consumed. An advantage of the presentinvention is the exploitation of the highly reactive nature of thereactive species produced from the catalytic media, oxygen and the newfuel from the organic matter instead of the enormous amounts of energythat are expended in producing a sufficiently hot incinerator to combustorganic materials and/or destroy the medical wastes by burning. Thisadvantage is particularly apparent in light of the extremely low cost ofcatalytic media such as silica or alumina, which are readily available,largely inert until exposed to the reactive conditions, and veryinexpensive.

Because of the nature of the conversion process, it is possible togreatly upscale or downscale the reactor size to accommodate a varietyof uses. The reaction apparatus and chamber may be very large in orderto serve large institutional needs such as a huge medical or researchcomplex as well as industrial energy production. Conversely, it may bevery small and portable when only required to destroy a small but steadystream of medical wastes or for local or personal energy production. Thelatter also provides for ease in moving and placement of the reactor inthe most convenient location.

Clean Energy Production

In one embodiment, the present invention includes methods forimplementing the reactor for efficiently and cleanly convertingcarbon-containing fuels such as fossil fuels into heat energy. However,other organic materials, such as biological wastes and municipal waste,can also be used for clean and efficient energy production with reactorsas described herein. The reactor can utilize catalytically reactiveparticles that are at least partially suspended by moving gases withinthe reaction chamber, and can be maintained at a temperature sufficientto cause the suspended media particles, typically silica sand, silicagel, or alumina, to produce reactive hydroxyl radicals, supercriticalwater, muon methyl radicals and/or other reactive species. The reactivespecies travel up into the void space above the catalytic media wherethey interact with the organic material supported by the supportelement. Typically, the reaction chamber can be maintained at atemperature in a range from about 420° C. to about 550° C. Moisture maybe provided by the organic mass.

Clean energy production includes means for converting energy intouseable energy such as heat and/or electricity. Traditionally, energycan be used for propulsion, heat, and generation of electricity. Assuch, the inventive reactor can be included within any system for energyproduction, where the reactor provides heat or exhaust gases that can beconverted by energy generation equipment into usable energy. Whilepropulsion energy may be obtained with the reactor, it may be moresuitable for generating heat and/or electricity. Accordingly, variousenergy generation and heat transfer equipment can be operably associatedwith the reactor so that the conversion of the organic material providesthe fuel source for energy production. Examples of energy generation andheat transfer can include the reaction chamber and even the supportelement to be thermally coupled to heat exchangers, steam generators, orother well known or later developed energy devices and systems. Thus,the reactor can be substituted for conventional combustion orincineration devices so that the organic material can be moreefficiently and cleanly used as fuel for energy production.

Degradation of Organic Waste

In one embodiment, the present invention includes methods for thecomplete and reliable destruction of biological materials such asmedical wastes or once-living human or animal tissues. Such methods notonly ensure the complete destruction of the actual physical or visiblewastes or tissues, but also ensure the complete destruction of allviruses, bacteria, or other pathogenic agents that might be found in themedical wastes or tissues. Moreover, such destruction is carried outwithout the need for chemical sterilization, autoclaving at hightemperature and pressure, high temperature incineration, plasma arcs,and the like. Instead, the present invention utilizes a reactor asdescribed herein that includes a reaction chamber containing a supportelement configured for maintaining the biological material at a distance(D) above the catalytic media. A reactive atmosphere can be generated bycatalytic particles, such as silica, alumina, and the like, wheninteracted with oxygen and pyrolysis products from the organic fuel. Themethod of destroying the biological materials can be performed asdescribed herein by placing the biological material on an elevatedsupport within the reaction chamber at a distance above the catalyticmedia so that the reaction gases can substantially completely convert ordegrade the organic material and decontaminate and destroy thebiological materials.

Because the biological material can be quickly and efficientlydisinfected and destroyed by the reactive gases in the reaction chamber,it greatly simplifies the heretofore significant problems associatedwith the disposal of medical wastes. It also provides a means for thecomplete disposal of animal or human corpses while generating lessbyproduct than the amount of ash produced by traditional cremation orincineration, which requires far more energy to carry out and which isknown to generate noxious or toxic gases.

In view of the foregoing, a feature of the present invention is toprovide methods and systems that result in the complete and reliabledestruction of medical wastes and other once-living human or animaltissue. Another feature is to provide methods and systems that result inthe complete and reliable destruction of medical wastes and otheronce-living human or animal tissue in a simple, single step withoutpolluting the environment. A further feature of the present invention isto provide methods and systems that ensure the complete destruction ofall viruses, bacteria, or other pathogenic agents that might be found inthe medical waste or corpse being disposed of. Yet another feature is toprovide methods and systems which completely and thoroughly destroy themedical waste or other once-living human or animal tissue without thegeneration of noxious gases. Still another feature of the presentinvention is to provide methods and systems that completely andthoroughly destroy the medical waste or other once-living human oranimal tissue at relatively low temperatures compared to conventionalincineration or plasma forming methods. Finally, it is a feature of thepresent invention to provide a reactor for carrying out the foregoingmethods that are relatively small and portable that could be stationedat a variety of locations within a hospital, research laboratory, orother sites where biological materials, medical wastes or corpses needto be destroyed without the possibility that dangerous viruses orpathogens are released into the environment, particularly at a hospitalor laboratory where sterile conditions are especially vital, or throughthe transport of such wastes to available landfill sites.

In one embodiment, the organic waste material can be from variousresearch, medical, or industrial applications as well as from deadanimals. As such, the organic waste material can include syringes, cellculture byproducts, bacteria broth byproducts, cell culture devicescontaminated with biological waste, dead tissue, dead animals, blood,body fluids, bacteria, viruses, or the like. In one aspect, the organicmaterial can be a dead human body, and the conversion process can beused in cremation.

In one embodiment, the conversion and/or degradation of biological wastematerials can be obtained by shutting of gas supply to the flame sourceafter a reaction zone at or above an elevated support reaches a firstdesired temperature so that the biological waste material issufficiently converted or degraded. Accordingly, once a desiredtemperature is achieved with aid of the flame source, the gas supply tothe flame source can be reduced or even turned off so that conversion ofthe organic waste material produces, maintains, or increases the desiredtemperature. As such, the energy production can be conducted whilemaintaining airflow in the absence of the flame source producing heatsuch that conversion of the organic material provides heat to reach ormaintain a second desired temperature. The second desired temperaturecan be the same or greater than the first desired temperature.

EXAMPLES Example 1

A reactor substantially as described herein was used in experiments toconvert and degrade organic materials ranging from cow bones, flesh, andPVC plastics in order to mimic other biological or medical wastes. Itwas found, surprisingly and unexpectedly, that the organic material doesnot have to physically contact the catalytic media as was previouslybelieved. It has now been surprisingly and unexpectedly found thatconversion and degradation of organic materials can be achieved bypositioning the organic material above the catalytic media such that theorganic material does not actually contact, and is not submerged withinthe volume of, the catalytic media. The organic materials in thisexample were not submerged into the silica bed but were ratherpositioned above the silica, suspended in a metal cage container. Theconversion reaction with the biological material appears to occur inabout a 2-36 inch zone above the silica bed. The conversion reaction notonly broke down the organic matter, it also converted the low energygrade materials (e.g., bones, plastic and biological waste materials)into a substantially higher amount of energy than would be expected bymere incineration as found by observing temperature increases in thereaction zone and void space above the catalytic media.

The conversion and energy production from biological waste materialswere conducted by introducing about 5 lbs of organic matter (e.g.,bones, flesh, and/or plastics) into a permeable container and thenlowering the container into the reaction chamber, with a lid placed overthe top of the reactor. Prior to placing the organic material into thereaction chamber, air was injected from the bottom, which passes throughthe silica, suspending the media. Natural gas was injected into thesilica media and ignited. The natural gas was used to heat the chamberto a temperature of 540° C. That temperature was reached inapproximately 20 seconds then the system automatically turned off thesupply of gas. Airflow was continuously injected into the reactionchamber as a continuous flow of ambient temperature air through thesystem.

At this point, the organic material was introduced into the chamber viaa container cage (e.g., support element) which was lowered into thechamber and a lid was placed on top. The temperature of the reactionchamber, as measured inside the silica bed, continued to climb toapproximately 870° C. as a result of the plasma reaction. In general,the temperature can stay between 540° C. and 920° C. for up to 40minutes after the gas to the flame source is turned off, though thetemperature is regulated to maintain an optimal 870° C. The temperatureis maintained with a continuous stream of cool, ambient air injectedthrough the bottom of the reaction chamber to maintain suspension of thecatalytic media.

Example 2

During conversion of organic waste materials, it was realized that asignificant amount of energy was being produced due to the increase andmaintenance of elevated temperatures. Accordingly, an experiment wasconducted to determine whether energy could be produced from highergrade solid fuels in, such as coal or charcoal. It was hypothesized thatthe process can enhance the release of energy in coal or other carbonfuel sources and obtain more consistent and higher sustainedtemperatures.

First, a baseline experiment was conducted to determine how fast thetemperature would rise and fall when the system is only injected withnatural gas as the heating element. This experiment showed that with gasonly, the systems temperature rose to 406° C., and without gas turnedon, but with air blowing through, cooled to 350° C. within 2 minutes, 13seconds.

Second, about 1½ lbs of charcoal were introduced into the reactionchamber using an elevated support. The system ran 20 minutes at 506° C.

Third, ½ lbs of charcoal were introduced into the reaction chamber ontothe elevated support, and temperature measurements in the reaction zonewere taken every minute.

The foregoing experiment only used ½ lb of charcoal and the systemmaintained a fairly consistent temperature range for the first 8minutes. However, it is believed that the silica bed began to getclumped up, which sometimes occurs and underlines the importance ofairflow diffusion and sufficient suspension of the catalytic mediawithout the media clumping. When media clumping occurs, the uneven flowof air seems to slow down the conversion reaction and possible thegeneration of reactive species from the catalytic media. At minute 17,the system cooled down to the point that it started automaticallyinjecting gas, but temperature continued to drop because of the unevenair flow. Then at minute 21, the airflow pressure was increased and thisrestored the silica and air flow. About 2 minutes later the gas wentoff, and there was another 8 minutes of sustained high temperature,which was even better than the first part of the experiment, until theall the material was depleted and the experiment was stopped.

From the foregoing, it can be determined that a very small amount oforganic material can maintain and even obtain a high temperature for asignificant amount of time. It can also be determined that since thereaction chamber is continuously being injected with cold air, theorganic material can sustain complete combustion, which furtherhighlights the consistency of the organic material maintaining a hightemperature. The baseline test shows that the air will rapidly cool thesystem from 406° C. to 350° C. in 2 minutes because of the temperatureof the air injected. Additionally, a proper flow of air through thesilica bed appears to be important for maintaining the conversionreaction and high temperature. When the airflow is disrupted, theconversion reaction appears to lessen and the temperature goes down, butmuch slower than the base line, which suggests that partial flowprovides a partial conversion reaction. Furthermore, it is thought thatrecirculation of exhaust gases or introducing hot air into the systemmay significantly increase the temperature and energy production becauseit will eliminate the cooling effect of cold air. Moreover, theconversion reaction occurs above the silica bed such that the silica bedcan now be reused without cleaning and removing remains of the organicmaterial. Thereafter, the elevated support can be cleaned and/or removedto remove the remains of the organic material.

It is thought that through the airflow having hydroxyl radicals,supercritical water, muons and/or other reactive species can interactwith the organic material in order to combust or otherwise react withthe organic matter, and thereby convert the organic materials into highamount of thermal energy.

The presently described systems and methods can be used for a low carbondioxide output process for producing electricity. Such a system andmethod can use a fraction of the volume of carbon fuel (e.g., coal) toobtain an equal amount of energy.

Moreover, the presently described systems and methods can be useful forconverting low grade fuel, trash, organic materials, or the like intohigh grade clean energy.

Example 3

10 lbs of Appalachian hard coal was tested in the center level of theinvention. Once the 540 C temperature was reached, the gas was shut offand the coal introduced into the device. The process ran for 90 minutesand maintained a temperature of 540 C to 570 C. without the natural gas.At the end of the experiment, the weight of the coal had been reducedfrom 10 lbs to 1 lb 8 oz and substantial amounts of energy had beenreleased with virtually no ash or emissions. The remaining material wasinert and inflammable.

Example 4

A semiconductor material for use in making microprocessors, computerchips, transistors, or photovoltaic solar cells is manufactured byproviding a substrate, such as those commonly used in the semiconductorindustry, and forming or depositing a single layer of a monomolecularnano film comprised of aligned carbon molecules having dimensions of 30angstroms by 50 angstroms and that elongate to 70 angstroms at highpressure resulting in substantial increase in temperature resistance,and operating capabilities.

The present invention may be embodied in other specific forms withoutdeparting from its spirit or essential characteristics. The describedembodiments are to be considered in all respects only as illustrativeand not restrictive. The scope of the invention is, therefore, indicatedby the appended claims rather than by the foregoing description. Allchanges which come within the meaning and range of equivalency of theclaims are to be embraced within their scope.

What is claimed is:
 1. A method for destroying medical waste and/or converting organic materials into thermal energy and/or electrical energy, the method comprising: providing a reactor comprising: a reaction chamber; a heat source in communication with the reaction chamber; an air source fluidly coupled with the reaction chamber; a catalytic media located within the reaction chamber so as to receive heat from the heat source and airflow from the air source; and an opening through the reaction chamber through which medical waste and/or organic material can be introduced into the reaction chamber; introducing heat and airflow into the reaction chamber so as to heat the reaction chamber to a first desired temperature; introducing medical waste and/or organic material into the reaction chamber and converting the medical waste and/or organic material into a fuel within the reaction chamber in the presence of the catalytic media, the fuel producing its own heat within the reaction chamber; and shutting off heat from the heat source while maintaining airflow to the reaction chamber, the heat from the fuel continuing to heat the reaction chamber so as to reach or maintain a second desired temperature that is the same or greater than the first temperature.
 2. The method of claim 1, wherein the reaction chamber has a cross-sectional dimension of from about 1 feet to about 100 feet.
 3. The method of claim 1, wherein the catalytic media within the reaction chamber includes a bed of particles that produce reactive species within the reaction chamber.
 4. The method of claim 3, wherein the particles are selected from silica sand, silica gel, hydroxylbastnasite, alumina, and combinations thereof.
 5. The method of claim 3, further comprising forming a monomolecular film on an interior surface of the reaction chamber.
 6. The method of claim 5, the monomolecular film on the interior surface of the reaction chamber enhancing formation of hydroxyl radicals, supercritical water, muons and/or other reactive species within the reaction chamber.
 7. The method of claim 1, wherein the medical waste and/or organic material comprises at least one member selected from the group consisting of organic waste, coal, fossil fuels, biomass, municipal waste, biological waste, cells, viruses, bacteria, severed tissue, blood, corpses, and combinations thereof.
 8. The method of claim 1, further comprising introducing additional heat to the reaction chamber from the heat source if the temperature within the reaction chamber drops below a predetermined minimum temperature.
 9. The method of claim 1, wherein the airflow includes unheated air.
 10. The method of claim 1, further comprising: providing a heat exchanger element thermally coupled with the reaction chamber; passing a heat exchanger fluid through the heat exchanger element so that heat produced within the reaction chamber heats the heat exchanger fluid; and generating electricity from the heated heat exchanger fluid.
 11. The method of claim 10, wherein electricity is generated from a steam generator thermally coupled with the heat exchanger element.
 12. The method of claim 1, further comprising: causing or allowing a plasma reaction to occur in the reaction chamber; and producing electrical energy from the plasma reaction.
 13. The method of claim 1, further comprising generating inert inorganic sterile materials from the medical waste and/or organic material.
 14. The method of claim 1, wherein converting medical waste and/or organic material comprises reducing and eliminating pollutants from diesel exhaust and increasing efficiency and output of a diesel engine.
 15. The method of claim 1, wherein converting medical waste and/or organic material comprises reducing and eliminating pollutants and emissions from and increasing efficiency of a coal fired electrical generation system.
 16. The method of claim 1, wherein converting medical waste and/or organic material comprises reducing and eliminating pollutants and emissions from a commercial waste incineration system.
 17. The method of claim 1, further comprising forming a monomolecular film on at least one substrate in communication with the reaction chamber.
 18. The method of claim 17, wherein the at least one substrate is selected from the group consisting of tools, electrical transmission wires, aircraft wing surface, and munitions.
 19. The method of claim 17, the monomolecular film comprising a semiconductor material.
 20. The method of claim 19, wherein the semiconductor material is suitable for use in making microprocessors, computer chips, transistors, or photovoltaic solar cells.
 21. The method of claim 20, the method forming a semiconductor chip comprising: the substrate; and a single layer of the monomolecular nano film comprised of aligned carbon molecules having dimensions of 30 angstroms by 50 angstroms and that elongate to 70 angstroms at high pressure resulting in substantial increase in temperature resistance and operating capabilities.
 22. A method for converting organic materials into thermal and electrical energy, the method comprising: providing a reactor comprising: a reaction chamber; a heat source in communication with the reaction chamber; an air source fluidly coupled with the reaction chamber; a catalytic media located within the reaction chamber so as to receive heat from the heat source and airflow from the air source; and an opening through the reaction chamber through which medical waste and/or organic material can be introduced into the reaction chamber; introducing heat and airflow into the reaction chamber so as to heat the reaction chamber to a first desired temperature; introducing organic material into the reaction chamber and converting the organic material into a fuel within the reaction chamber in the presence of the catalytic media, the fuel producing its own heat within the reaction chamber; shutting off heat from the heat source while maintaining airflow to the reaction chamber, the heat from the fuel continuing to heat the reaction chamber so as to reach or maintain a second desired temperature that is the same or greater than the first temperature; and producing or collecting electrical energy.
 23. The method of claim 22, wherein producing or collecting electrical energy comprises: providing a heat exchanger element thermally coupled with the reaction chamber; passing a heat exchanger fluid through the heat exchanger element so that heat produced within the reaction chamber heats the heat exchanger fluid; and generating electricity from the heated heat exchanger fluid.
 24. The method of claim 22, wherein producing or collecting electrical energy comprises: causing or allowing a plasma reaction to occur in the reaction chamber; and collecting electrical energy from the plasma reaction.
 25. A method for converting organic materials into thermal energy and, the method comprising: providing a reactor comprising: a reaction chamber; a heat source in communication with the reaction chamber; an air source fluidly coupled with the reaction chamber; a catalytic media located within the reaction chamber so as to receive heat from the heat source and airflow from the air source; and an opening through the reaction chamber through which medical waste and/or organic material can be introduced into the reaction chamber; introducing heat and airflow into the reaction chamber so as to heat the reaction chamber to a first desired temperature; introducing organic material into the reaction chamber and converting the organic material into a fuel within the reaction chamber in the presence of the catalytic media, the fuel producing its own heat within the reaction chamber; shutting off heat from the heat source while maintaining airflow to the reaction chamber, the heat from the fuel continuing to heat the reaction chamber so as to reach or maintain a second desired temperature that is the same or greater than the first temperature; and providing a monomolecular film on at least one substrate in communication with the reaction chamber, the monomolecular film comprising a semiconductor material.
 26. The method of claim 25, wherein the semiconductor material comprises comprising: the substrate; and a single layer of the monomolecular nano film comprised of aligned carbon molecules having dimensions of 30 angstroms by 50 angstroms and that elongate to 70 angstroms at high pressure resulting in substantial increase in temperature resistance and operating capabilities. 